CN105463147A - Method for producing nickel iron powder by directly reducing nickel laterite ores in rotary kiln - Google Patents
Method for producing nickel iron powder by directly reducing nickel laterite ores in rotary kiln Download PDFInfo
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- CN105463147A CN105463147A CN201510422624.7A CN201510422624A CN105463147A CN 105463147 A CN105463147 A CN 105463147A CN 201510422624 A CN201510422624 A CN 201510422624A CN 105463147 A CN105463147 A CN 105463147A
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Abstract
The invention discloses a method producing nickel iron powder by directly reducing nickel laterite ores in a rotary kiln. The method comprises the following steps: carrying out primary crushing, drying, carrying out secondary crushing, mixing, pressing materials into balls, carrying out roasting reduction in the rotary kiln, carrying out tertiary crushing, carrying out ball-milling, and carrying out primary magnetic separation, thereby finally obtaining the nickel iron powder. According to the method, mixed materials are fed into the rotary kiln for being reduced after being pressed into balls, so that sintering is relatively sufficient, and nickel grade of the obtained nickel iron powder is 10% or higher, up to 15%, a nickel recovery rate is 90% or higher, up to 97%, iron grade is 80% or higher, up to 85%, and an iron recovery rate is 80% or higher, up to 90%. Besides, in case of less dosage of limestone powder, slag phase basicity and viscosity, and a liquid phase of roasted materials in the kiln can be regulated very well, so that reaction can be sufficiently carried out, viscosity of the liquid phase in the kiln is kept good, a kiln sticking phenomenon is relieved, and the kiln wall is not liable to thicken and to form a ring.
Description
Technical field
The invention belongs to the manufacturing technology field of ferronickel powder, produce the method for ferronickel powder in particular to a kind of direct reduction of laterite nickel mine with rotary kiln.
Background technology
At present, ferronickel powder is as a kind of metal powder material, owing to possessing good surfactivity, chemical stability, electrical and thermal conductivity, can weld and feature and the relative low price such as soldering resistance, replace the precious metals such as gold and silver in recent years gradually and be applied to catalystic material, electrode materials and Wimet etc.Such as current electrode materials, adopts ferronickel powder as raw material, to prepare lithium nickelate combination electrode material more.Meanwhile, ferronickel powder is also one of raw material of stainless steel product.
Ferronickel powder has multiple preparation method, comprises nickle carbonoxide thermal decomposition method, evaporation-condensation method, alloyage, gas reduction method, electrolytic process, mechanical crushing method and liquid phase reduction etc.In these methods, technique is simple, raw material is easy to get, form features such as being easy to control, particle size is little, granularity is controlled owing to having for liquid phase reduction, becomes and prepares the important method of ferronickel powder one class in recent years.In this method, often select hydrazine as reductive agent.Existing a kind of preparation technology adopts extracting and separating to obtain nickelous chloride raw material, and through the synthesis of presoma, high temperature reduction two sections of operations, produce ferronickel powder.Wherein presoma comprises nickelous carbonate or nickelous oxalate etc., and this technique building-up process produces the waste water of nickeliferous and ammonia nitrogen in a large number, not only reduces the rate of recovery of metal, and needs special Waste Water Treatment.And these presomas all introduce carbon, thus in final product, have higher carbon content, be an important source of nickel powder Cost Problems and quality problems simultaneously.In addition, also some adopts the nickel powder that carbonyl process is produced, and is commonly referred to as carbonyl nickel powder, such as Canadian Inco produces carbonyl nickel powder, include the series product such as T255, T123, be also containing carbon in the raw material of these carbonyl nickel powder products, do not meet the environmental requirement of current low-carbon (LC).
Method using red soil nickel ore as raw material enriching nickel iron powder mainly contains: thermal process, wet processing, fiery wet method combined process.Wherein thermal process is mainly blast furnace and rotary kiln-electrosmelting.The outer reducing and smelting ferronickel technique of stove, not only requires that the taste of red soil nickel ore is high, and needs to consume a large amount of energy, also has requirement to the silicon magnesium ratio of raw material.Wet processing, i.e. sulfuric acid pressure leaching process, although realize suitability for industrialized production at present, but because it adopts condition of high voltage to operate, equipment, scale, investment, operation control and ore grade, magnesium oxide etc. are had higher requirements, extract metallic nickel by pickling process, not only cost is high but also produce a large amount of waste liquid, causes severe contamination to environment.Fire wet method combined process, mainly raw ore reduction roasting-ammonia leaching technique, process low-grade laterite nickel ore, but the rate of recovery is low, cost is high.Above-mentioned processing unit is not only invested greatly, energy consumption is many, and its ferronickel grade produced is also lower.
Summary of the invention
For the deficiencies in the prior art, a kind of direct reduction of laterite nickel mine with rotary kiln is the object of the present invention is to provide to produce the method for ferronickel powder.Processing method of the present invention can adjust the liquid phase of calcining materials in slag phase basicity, viscosity, adjustment kiln well, reaction can fully be carried out, the viscosity of liquid phase in kiln can be kept simultaneously well, prevent sticky kiln and make the long thick ring formation of kliner coating, thus increasing production efficiency.In addition, the ferronickel powder that the inventive method is produced can be directly used in manufacture stainless steel.
To achieve these goals, present invention employs following technical scheme:
Direct reduction of laterite nickel mine with rotary kiln produces a method for ferronickel powder, comprises primary crushing, oven dry, second time fragmentation, mixing, pressure ball, rotary kiln baking reduction, third time fragmentation, ball milling and first time magnetic separation step, finally obtains ferronickel powder, wherein:
In described primary crushing step, it is below 80mm that raw material red soil nickel ore is crushed to raw meal particle size;
In described baking step, red soil nickel ore after primary crushing is dried, described bake out temperature is 750 DEG C ~ 850 DEG C (such as 760 DEG C, 800 DEG C, 820 DEG C, 840 DEG C, preferably 800 DEG C), and drying time is 15-25min (such as 16min, 20min, 22min);
In described second time destruction step, by red soil nickel ore secondary breaking to the raw meal particle size after drying be below 3mm account for more than 80%, thus obtain the suitable dry ore deposit of granularity;
In described mixing step, by described dry ore deposit and reductive agent carbon, limestone powder mixes, add water simultaneously, thus formation mixture, wherein, described dry ore deposit accounts for described dry ore deposit, the 85-92wt% (such as 86% of reductive agent carbon and limestone powder gross weight, 88%, 89%, 90%, 91%), described reductive agent carbon accounts for described dry ore deposit, the 5-12wt% (such as 6% of reductive agent carbon and limestone powder gross weight, 8%, 9%, 10%, 11%), described limestone powder accounts for described dry ore deposit, the 1-3wt% (such as 1.2% of reductive agent carbon and limestone powder gross weight, 1.5%, 2%, 2.3%, 2.8%), the water content of described mixture is 14-16wt% (such as 14.5%, 15%, 15.5%),
In described pressure ball step, described mixture is pressed into pelletizing;
In described rotary kiln baking reduction step, described pelletizing is sent in rotary kiln from above-mentioned rotary kiln feed-pipe, after super-dry, preheating, reducing roasting three phases, falls into dragveyer from kiln hood exit carry out Water Quenching, thus obtain agglomerate; Wherein, the temperature of described dryer section controls at 200 ~ 350 DEG C (such as 210 DEG C, 250 DEG C, 280 DEG C, 310 DEG C, 320 DEG C, 330 DEG C, 345 DEG C); The temperature of described preheating section controls at 350 ~ 600 DEG C (such as 355 DEG C, 370 DEG C, 450 DEG C, 500 DEG C, 520 DEG C, 550 DEG C, 580 DEG C); The temperature of described reducing roasting section controls at 600 ~ 1350 DEG C (such as 620 DEG C, 700 DEG C, 750 DEG C, 900 DEG C, 1000 DEG C, 1100 DEG C, 1200 DEG C, 1300 DEG C, 1340 DEG C), and the total time that described pelletizing stops in whole rotary kiln is 4-6h.
In the above-mentioned methods, raw material red soil nickel ore is low-grade red soil nickel ore, and water content is about 35%, in order to the pellet quality that the water content and pressure ball step that control the dry ore deposit used in above-mentioned mixing step better obtain, the present invention, when processing raw material red soil nickel ore, adopts the broken mode of preliminary fragmentation-oven dry-second time to obtain the dry ore deposit that granularity is suitable, content hydration is suitable.Find through overtesting, compared to omission baking step, adopt the dry ore deposit after drying to make pelletizing, more abundant at rotary kiln baking reduction phase sintering, metal recovery rate is higher.
In the above-mentioned methods, as a kind of preferred implementation, in described baking step, the partial heat described in drying plant is from the waste heat at described rotary kiln mouth place.
In the above-mentioned methods, as a kind of preferred implementation, in described pressure ball step, described pelletizing is of a size of 43 × 42 × 25mm.
In the above-mentioned methods, as a kind of preferred implementation, in described rotary kiln baking reduction step, described pelletizing is 2.5-3h (2.6h, 2.8h, 2.9h) in the time that described reducing roasting section stops.
In the above-mentioned methods, as a kind of preferred implementation, the specification of described rotary kiln is the inclined type rotary rotary kiln of Ф 3.6 × 72m, and the gradient of rotary kiln is 2.5%, and kiln body rotating speed is 0.2-1.8r/min.
In the above-mentioned methods, as a kind of preferred implementation, in described rotary kiln baking reduction step, the heat of described rotary kiln comes from the heat of injection from kiln head bunker coal burning generation.The traffic direction of such heat and the traffic direction of pelletizing just the opposite, thus realize the abundant sintering of pelletizing.
In the above-mentioned methods, as a kind of preferred implementation, in described third time destruction step, described agglomerate is carried out be crushed to raw meal particle size be below 3mm account for more than 90%.
In the above-mentioned methods, as a kind of preferred implementation, in described ball milling step, the agglomerate after third time fragmentation carries out wet ball grinding, after ball milling the granularity of agglomerate be below 120 orders account for more than 80%;
In the above-mentioned methods, as a kind of preferred implementation, in described first time magnetic separation step, the ore deposit pulp density entering magnetic separator is 25-30% (such as 26%, 28%, 29%), after described first time magnetic separation, obtain high-grade ferronickel powder.More preferably, the magneticstrength of described magnetic separator is 1600-5000GS (such as 1800GS, 2500GS, 3000GS, 3500GS, 4000GS, 4500GS, 4900GS).
In the above-mentioned methods, as a kind of preferred implementation, tramp iron separator magnetic separation step is set between described third time fragmentation and described ball milling, adopts tramp iron separator to carry out magnetic separation to the agglomerate after described third time fragmentation, to select part of nickel iron powder from the broken last agglomerate after third time fragmentation.So also can reduce the operating pressure of next step ball mill device.
In the above-mentioned methods, as a kind of preferred implementation, described reductive agent carbon is pulverized anthracite.
Adopt aforesaid method can be directly used in manufacture stainless steel from the ferronickel powder of red soil nickel ore direct-reduction enrichment.Processing method of the present invention is directly reduced sending in rotary kiln after mixture pressure ball, and sintering is relatively more abundant, in the production process of ferronickel powder, each 3h carries out sampling analysis, in the proof procedure of continuous 1 year, nickel grade, all more than 10%, reaches as high as 15%; Nickel recovery all reaches more than 90%, reaches as high as 97%; Iron grade all reaches more than 80%, reaches as high as 85%; Iron recovery all reaches more than 80%, reaches as high as 90%.
In addition, in rotary kiln baking reduction step, additive of the present invention and limestone powder still can adjust the liquid phase of calcining materials in slag phase basicity, viscosity, adjustment kiln well when consumption is little, reaction can fully be carried out, in kiln, the viscosity of liquid phase keeps good, sticky kiln phenomenon is eased, and kiln wall is long thick ring formation not easily, thus adds production efficiency.
In addition, the grade of present invention process to red soil nickel ore does not have excessive demand, and the nickelic laterite of the low nickel of low iron, low iron all can produce the ferronickel powder that nickel content is greater than 10%.Preferably, as a kind of preferred implementation, mass ratio≤10 of the nickel content of described red soil nickel ore to be 1.5 ~ 2.3wt%, TFe content be 14 ~ 22wt%, TFe and Ni.
Direct reduction of laterite nickel mine with rotary kiln produces a system for ferronickel powder, and described system comprises: the first shredder assembly, and described first shredder assembly is used for raw material red soil nickel ore to carry out fragmentation; Drying unit, the admission port of described drying unit is connected by the relief outlet of belt conveyor with described first shredder assembly, dries for the red soil nickel ore by described first shredder assembly conveying after next fragmentation; Second shredder assembly, the admission port of described second shredder assembly is connected by the relief outlet of belt with described drying unit, carries out again broken, obtain dry ore deposit for the red soil nickel ore by described drying unit conveying after next oven dry; Mixing device, the admission port of described mixing device is connected by the relief outlet of belt with described second shredder assembly, for forming mixture by after dry ore deposit and reductive agent carbon, limestone powder, water Homogeneous phase mixing; Ball press, entrance is connected with the outlet of described mixing device, and mixture is pressed into oval spherical i.e. pelletizing; Rotary kiln, the feed-pipe of described rotary kiln is connected with the relief outlet of described ball press, for forming agglomerate by after pellet sintering; Submerged slag conveyor, is arranged at described rotary kiln end exit, for carrying out shrend by from rotary kiln material out and pull out from water, thus obtains agglomerate; 3rd shredder assembly, admission port is connected with described submerged slag conveyor by belt, broken for agglomerate being carried out third time, and makes the granularity of the agglomerate after fragmentation account for more than 90% at below 3mm; Ball mill device, the admission port of described ball mill device is connected by the relief outlet of belt with described 3rd shredder assembly, for the agglomerate after third time fragmentation is carried out wet ball grinding, makes the granularity of the agglomerate after ball milling account for more than 80% below 120 orders; With the first concentration equipment, the admission port of described first concentration equipment is connected by the relief outlet of belt with described ball mill device, for carrying out magnetic separation to the agglomerate after ball milling, to obtain ferronickel powder.
Preferably, in the system, also comprise the second concentration equipment, described second concentration equipment is arranged on the relief outlet place of described 3rd shredder assembly, for magneticly electing part of nickel iron powder.Material after described second concentration equipment magnetic separation enters in ball mill device and carries out wet ball grinding to reduce the pressure of ball mill.More preferably, described second concentration equipment is tramp iron separator.
Preferably, in the system, also comprise described electric precipitator, described electric precipitator is arranged on the admission port position of described drying unit, for absorbing the dust of described drying unit emission, makes tail gas qualified discharge.
Preferably, in the system, also comprise: high-temperature blower, described high-temperature blower is located at the kiln tail mouth place of described rotary kiln, for the high-temperature flue gas of described rotary kiln is guided to described drying unit, high-temperature flue gas carries out drying treatment the red soil nickel ore after the fragmentation in described drying unit.
Preferably, in the system, also comprise: pass air pipe, the two ends of described biography air pipe are connected to the outlet of described high-temperature blower and the admission port position of described drying unit, for being delivered in described drying unit by the hot blast of described high-temperature blower.
Preferably, in the system, also comprise: mixing bunker, described mixing bunker is arranged on the front end of described mixing device.
Preferably, in the system, also comprise: the first fly-ash separator, the first cone pump and ashes belt, the two ends of described first cone pump are connected with the entrance end of described ashes belt with the exit end of described first fly-ash separator respectively, described first fly-ash separator is located at the top of described second shredder assembly, the entrance end of described first fly-ash separator towards described second shredder assembly, for absorbing the dust in described second shredder assembly; The exit end of described ashes belt is connected with the entrance end of described mixing bunker, for being delivered in described mixing bunker by dust.
Preferably, in the system, also comprise: the second fly-ash separator and the second cone pump, the exit end of described second fly-ash separator is connected with the entrance end of described second cone pump, the entrance end of described second fly-ash separator is arranged on above the relief outlet of described mixing device, for absorbing the dust in described mixing device; The exit end of described second cone pump is connected with the entrance end of described ashes belt.
Preferably, in the system, also comprise: dust excluding hood, described dust excluding hood is arranged on the upper end of described mixing bunker.
This system can be used for realizing the method that above-mentioned direct reduction of laterite nickel mine with rotary kiln produces ferronickel powder.
Analyze known, compared with prior art, system of the present invention adopt raw material red soil nickel ore carried out first time broken, dry, second time fragmentation, mixing, pressure ball, sintering, again fragmentation, ball milling and magnetic separation process obtain containing the more concentrate of ferronickel powder, then unclassified stores is utilized again.Whole system one body running of the present invention completes and obtains nickel powder, gets involved without the need to other devices, can complete separately the extraction of nickel powder.Moreover system of the present invention also comprises cleaning apparatuss such as being provided with electric precipitator, the first fly-ash separator and the second fly-ash separator, the dust of manufacturing processed can be carried out collection and treatment again, meet the requirement of protection of the environment, can not cause environmental pollution states.Moreover the present invention can realize zero release standard again while having production efficiency.Compare other pyrogenic process nickel-iron smelting production systems energy-conservation more than 40%.
Accompanying drawing explanation
Fig. 1 is the process flow sheet of the inventive method preferred embodiment.
Fig. 2 is the structural representation of present system preferred embodiment.
A-raw material red soil nickel ore; B-does ore deposit; C-agglomerate; 1-first shredder assembly; The thick bar grizzl(e)y of 11-; 2-drying unit; 21-electric precipitator; 3-second shredder assembly; 31-first circular shale shaker; 32-does ore deposit crusher; 33-second circular shale shaker; 34-fine crusher; 35-first fly-ash separator; 36-first cone pump; 4-mixing device; 41-mixing bunker; 42-dust excluding hood; 43-second fly-ash separator; 44-second cone pump; 45-ashes belt; 46-metering device; 5-rotary kiln; 51-ball press; 52-high-temperature blower; 53-first quantitatively claims; 6-the 3rd shredder assembly; 61-primary mill; 62-type fine disintegrating machine; 63-four-roller crusher; 7-ball mill device; 71-second quantitatively claims; 72-the 3rd concentration equipment; 8-first concentration equipment; 81-concentrate pond; 82-tailings pond; 9-second concentration equipment.
Embodiment
Below in conjunction with the drawings and specific embodiments, the present invention is described in further details.
As shown in Figure 1, the preferred direct reduction of laterite nickel mine with rotary kiln of the present invention produces the system of ferronickel powder, mainly comprises the first shredder assembly 1, drying unit 2, second shredder assembly 3, mixing device 4, rotary kiln 5, the 3rd shredder assembly 6, ball mill device 7 and the first concentration equipment 8; Raw material red soil nickel ore A forms dry ore deposit B after being worked by the first shredder assembly 1, drying unit 2 and the second shredder assembly 3, dry ore deposit B forms agglomerate C by after mixing device 4, ball press, rotary kiln 5, dragveyer work, and agglomerate C is again by obtaining nickel powder after work after the 3rd shredder assembly 6, ball mill device 7 and the first concentration equipment 8.
Specifically, as shown in Figure 2, the red soil nickel ore after fragmentation for raw material red soil nickel ore A is broken, and is delivered to drying unit 2 by the first shredder assembly 1, drying unit 2 is dried for the red soil nickel ore after the fragmentation of being carried by the first shredder assembly 1, and the red soil nickel ore after drying is delivered to the second shredder assembly 3, second shredder assembly 3 carries out again broken for the red soil nickel ore after the oven dry of being carried by drying unit 2, obtain dry ore deposit B, and dry ore deposit B is delivered to mixing device 4, mixing device 4 will do ore deposit B and reductive agent coal dust, limestone powder, form mixture after water Homogeneous phase mixing and mixture is pressed into spherical after be delivered to rotary kiln 5, rotary kiln 5 is for by spherical mixture and pellet sintering, material after sintering falls into dragveyer after shrend, forms agglomerate C, agglomerate C is delivered to the 3rd shredder assembly 6, 3rd shredder assembly 6 is broken for agglomerate C being carried out third time, the granularity of the agglomerate C after fragmentation is made to account for more than 90% at below 3mm, again the agglomerate C after fragmentation is delivered to ball mill device 7, ball mill device 7, for the agglomerate C after fragmentation is carried out wet ball grinding, makes the granularity of the agglomerate C after ball milling account for more than 80% below 120 orders, then the agglomerate C after ball milling is delivered to the first concentration equipment 8, agglomerate C after first concentration equipment 8 pairs ball milling carries out magnetic separation, obtains high-grade nickel iron powder.
When the 3rd shredder assembly 6 couples of agglomerate C carry out fragmentation, the powder that broken agglomerate C meeting forming section granularity is less, these powder are delivered to the operating pressure that ball mill device 7 ball milling can strengthen ball mill device 7 again, and also can not play the effect of ball milling to these broken ends; Based on this, the present invention is preferably provided with the second concentration equipment 9 at the relief outlet place of the 3rd shredder assembly 6, for magneticly electing part of nickel iron powder.In order to prevent the second concentration equipment 9 from impacting the 3rd shredder assembly 6, the second concentration equipment 9 is preferably tramp iron separator.
In order to ensure that the granularity of the raw material red soil nickel ore A entered in drying unit 2 can not be excessive, be provided with thick bar grizzl(e)y 11 in the outlet of the first shredder assembly 1.The size of mesh granularity of thick bar grizzl(e)y 11 is preferably 80mm.First shredder assembly 1 by the Task-size Controlling after raw material red soil nickel ore A fragmentation at below 80mm.Preferably, the first shredder assembly 1 is wet ore deposit crusher.
In order to adapt to the raw material red soil nickel ore A of drying granularity comparatively large (if granularity is at 80mm), drying unit 2 is preferably drying kiln (or dry kiln or dryer), material delivering plate is provided with in drying kiln, sent into from the admission port of drying kiln by the raw material red soil nickel ore A after the first shredder assembly 1 fragmentation, by material delivering plate, the raw material red soil nickel ore A after oven dry is delivered to the relief outlet of drying kiln.
In order to reduce the powder of the raw material red soil nickel ore A in drying unit 2 to environment, be provided with electric precipitator 21 in drying unit 2 admission port position.Certainly also there will be the situation of airborne dust when excavating raw material red soil nickel ore A, being provided with electric precipitator 21 equally in the excavation site of raw material red soil nickel ore A.The present invention is only for electric precipitator 21, as long as certain any device that can prevent airborne dust.
In order to effectively the red soil nickel ore after oven dry be carried out fragmentation, second shredder assembly 3 of the present invention comprises dry ore deposit crusher 32 and fine crusher 34, dry ore deposit crusher 32 is placed in fine crusher 34 front, carries out broken for the red soil nickel ore after being dried by drying unit 2 again; Red soil nickel ore granularity after in small, broken bits, for the red soil nickel ore after crusher 32 fragmentation of dry ore deposit is carried out process in small, broken bits, is accounted for more than 80% at below 3mm by fine crusher 34.Preferably, dry ore deposit crusher 32 is hammer mill, and fine crusher 34 is Europe version efficient fine crusher.
Effectively fragmentation can be carried out for the ease of red soil nickel ore, the present invention also comprises the first circular shale shaker 31, first circular shale shaker 31 is arranged on the admission port position of dry ore deposit crusher 32, and the red soil nickel ore for sieve aperture granularity being less than the first circular shale shaker 31 screens and is delivered to mixing device 4.
Can effectively carry out in small, broken bits for the ease of red soil nickel ore, the present invention also comprises the second circular shale shaker 33, second circular shale shaker 33 is arranged on the admission port position of fine crusher 34, and the red soil nickel ore for sieve aperture granularity being less than the second circular shale shaker 33 screens and is delivered to mixing device 4.
Can carry out pre-mixing in advance in order to ensure the mixture entering mixing device 4, also comprise mixing bunker 41, mixing bunker 41 is arranged on the front end of mixing device 4.
Realize, in dry ore deposit B and reductive agent coal dust, limestone powder, water pre-mixing process, there will be the situation that dust raises up, in order to prevent dust from impacting environment, also comprising dust excluding hood 42, being arranged on the upper end of mixing bunker 41 in mixing bunker 41.
If the pre-mixing material held in mixing device 4 too much can affect the mixing of pre-mixing material, be unfavorable for that the follow-up mixture to mixing device 4 discharge processes, if the pre-mixing material held in mixing device 4 is very few, waste resource can be caused again, dry ore deposit B, coal dust, limestone powder, water are weighed simultaneously, carry out pre-mixing according to the certain proportion preset separately to make it; Based on this problem, system provided by the invention also comprises metering device 46, and metering device 46 is arranged between mixing bunker 41 and mixing device 4, and for carrying quantitative pre-mixing material toward mixing device 4, metering device 46 is preferably constant feeder.
When the mixture of discharging mixing device 4 in rotary kiln 5 sinters, if the volume difference of mixture is larger, part mixes material then can be caused to have sintered, the situation that another part mixture does not also fully sinter, in the face of this problem, system provided by the invention also comprises ball press 51, ball press 51 is arranged between mixing device 4 and rotary kiln 5, mixture for being discharged by mixing device 4 is pressed into uniform ball shape, and the mixture of ball shape and pelletizing is delivered in rotary kiln 5.Further, system provided by the invention also comprises high-temperature blower 52, and be located at the kiln tail exit of rotary kiln 5, for the high-temperature flue gas of rotary kiln 5 is guided to drying unit 2, high-temperature flue gas carries out drying treatment the red soil nickel ore after fragmentation in drying unit 2.
In order to prevent system provided by the invention to environment further and reduce energy consumption (low stain and low consumption), the present invention also comprises biography air pipe, the two ends passing air pipe are connected to the outlet of high-temperature blower 52 and the admission port position of drying unit 2, for the hot blast of high-temperature blower 52 is delivered in drying unit 2, realize the utilization again high-temperature blower 52 being produced to a large amount of hot blast, namely the waste heat (exporting with the form of flue gas) exported by rotary kiln 5 by high-temperature blower 52 is delivered in drying unit 2, drying unit 2 is made to utilize this waste heat to dry raw material red soil nickel ore A.
In order to ensure effectively to sinter the mixture being pressed into ball shape in rotary kiln 5, the present invention also comprises first and quantitatively claims 53, is arranged on the entrance end of rotary kiln 5, for conveying mixture in quantitatively past rotary kiln 5.
In order to prevent the dust formed in the second shredder assembly 3 to environment, the present invention also comprises the first fly-ash separator 35, first cone pump 36 and ashes belt 45, the two ends of the first cone pump 36 are connected with the entrance end of ashes belt 45 with the exit end of the first fly-ash separator 35 respectively, first fly-ash separator 35 is located at the top of the second shredder assembly 3, the entrance end of the first fly-ash separator 35 towards the second shredder assembly 3, for absorb second shredder assembly 3 row become dust; The exit end of ashes belt 45 is connected with the entrance end of mixing bunker 41, for being delivered in mixing bunker 41 by dust.In order to prevent the dust formed in ball press 51, mixing device 4 to environment, the present invention also comprises the second fly-ash separator 43 and the second cone pump 44, the exit end of the second fly-ash separator 43 is connected with the entrance end of the second cone pump 44, the entrance end of the second fly-ash separator 43 is separately positioned on above the top of ball press 51 and the relief outlet of mixing device 4, for absorbing the dust of ball press 51 and mixing device 4 formation; The exit end of the second cone pump 44 is connected with the entrance end of ashes belt 45.In order to the airborne dust collected dust excluding hood 42 effectively processes, the exit end of dust excluding hood 42 is connected with the entrance end of the second cone pump 44.Ashes belt 45 can certainly be divided into the first ashes belt and the second ashes belt, the first ashes belt is arranged between the first cone pump 36 and mixing bunker 41, and the second ashes belt is arranged between the second cone pump 36 and mixing bunker 41.
In order to agglomerate C being carried out effective fragmentation, 3rd shredder assembly 6 of the present invention comprises primary mill 61, type fine disintegrating machine 62 and four-roller crusher 63, the admission port of type fine disintegrating machine 62 is connected with the relief outlet of primary mill 61, and the relief outlet of type fine disintegrating machine 62 is connected with the admission port of four-roller crusher 63; The admission port of primary mill 61 is connected with the relief outlet of rotary kiln 5, and the relief outlet of four-roller crusher 63 is connected with the admission port of ball mill device 7.In order to more obtain nickel powder, be respectively equipped with the second concentration equipment 9 at the relief outlet of primary mill 61, type fine disintegrating machine 62 and four-roller crusher 63.
In order to the agglomerate C after ensureing the 3rd shredder assembly 6 fragmentation can be impartial be delivered to ball mill device 7, the present invention also comprises second and quantitatively claims 71, second quantitatively claims 71 to be arranged between the 3rd shredder assembly 6 and ball mill device 7, for quantitatively carrying the agglomerate C after fragmentation in ball mill device 7.In order to obtain ferronickel powder further, the present invention also comprises the 3rd concentration equipment the 72, three concentration equipment 72 and is arranged on the ingress that second quantitatively claims 71, for magneticly electing ferronickel powder.3rd concentration equipment 72 and the second concentration equipment 9 are preferably tramp iron separator, can be belt-type permanentmagnet tramp iron separator, electric magnetic iron remover or permanent magnetic wheels tramp iron separator.First concentration equipment 8 is preferably magnetic separator.
In order to carry out bulk treatment to the sintering mineral aggregate after the first concentration equipment 8 magnetic separation, the present invention also comprises concentrate pond 81 and tailings pond 82, first concentration equipment 8 magnetic separation ferronickel powder is out delivered in concentrate pond 81, and the remaining mineral aggregate of the first concentration equipment 8 is delivered in tailings pond 82.
In order to process to reclaim fine ore to this slag before being delivered to tailings pond by the isolated slag of the first concentration equipment 8, the exit of the first concentration equipment 8 is provided with tailings recovery device, realize the recycling again to fine ore, it is preferably refuse ore reclaiming machine.
In order to be described in detail to system of the present invention, also be that the method in order to produce ferronickel powder to direct reduction of laterite nickel mine with rotary kiln of the present invention is described in detail, exemplifying several specific embodiment below.
The reductive agent hard coal used in following examples and the main component of fuel bituminous coal as follows:
The anthracitic main component of reductive agent:
Fixed carbon: 63.36wt%, ash content: 17.6wt%, volatile matter: 7.04wt%, P:0.015wt%, S:0.70wt%, H2O:12.0wt%, granularity: 5-30mm.
The main component of fuel bituminous coal:
Fixed carbon: 48.0wt%, ash content: 11.32wt%, volatile matter: 28.0wt%, P:0.015wt%, S:0.75wt%, H2O:12.5wt%, granularity: 5-30mm.
Embodiment 1
The main component of the raw material red soil nickel ore of the present embodiment:
Ni：1.8-1.9wt％，Fe：15-18wt％，SiO
2：35wt％，MgO：22.5wt％，H
2O：30-35wt％。
(1) primary crushing: delivered to by above-mentioned raw materials red soil nickel ore in the crusher of wet ore deposit, being crushed to raw meal particle size is below 80mm.
(2) dry: the red soil nickel ore after primary crushing is delivered to oven dry kiln dry, and bake out temperature is about 800 DEG C, and drying time is 25min; Heat in drying kiln is from the waste heat at rotary kiln mouth place and blast furnace gas combustion.
(3) second time is broken: by the red soil nickel ore after drying successively through hammer mill and Europe version efficient fine crusher, thus its second time is crushed to raw meal particle size be below 3mm account for more than 80%, thus obtain the suitable dry ore deposit of granularity;
(4) mix: dry ore deposit is mixed with reductive agent pulverized anthracite, limestone powder, add water simultaneously, thus form mixture, wherein, the mass ratio of dry ore deposit, coal dust and limestone powder is about 89:8:3, and the water content of mixture is about 15wt%;
(5) pressure ball: adopt ball press that mixture is carried out pressure ball process, the size control of gained pelletizing is at about 43 × 42 × 25mm; Pelletizing is excessive or too smallly all have a negative impact to roasting reduction effect, can reduce the rate of recovery and the grade of ferronickel;
(6) roasting reduction: described pelletizing is sent in rotary kiln from rotary kiln feed-pipe, falls into dragveyer from kiln hood exit and carry out Water Quenching after super-dry, preheating, roasting reduction three phases, thus obtain agglomerate; Wherein, dryer section temperature is at 200 ~ 350 DEG C; Preheating section temperature is at 350 ~ 600 DEG C; Reducing roasting section temperature is at 600 ~ 1350 DEG C, and the total time that pelletizing stops in rotary kiln is 5h, and the time controling that pelletizing stops in reducing roasting section is at about 2.8h.The specification of rotary kiln is the inclined type rotary rotary kiln of Ф 3.6 × 72m, and the gradient of rotary kiln is 2.5%, and kiln body rotating speed is 0.5r/min.The heat that the heat of rotary kiln produces from injection from kiln head coal combustion.
(7) third time is broken: described agglomerate is successively through primary mill, type fine disintegrating machine 62 and four-roller crusher, and to be carried out by agglomerate being crushed to raw meal particle size, to be below 3mm account for more than 90%.
(8) tramp iron separator magnetic separation: adopt tramp iron separator to carry out magnetic separation to the material after described third time fragmentation, to select ferronickel powder from the broken last material after third time fragmentation.So also can reduce the operating pressure of next step ball mill device.
(9) ball milling: the agglomerate after third time fragmentation carries out wet ball grinding, after ball milling the granularity of agglomerate be below 120 orders account for more than 80%;
(10) first time magnetic separation: sent in magnetic separator by the material after ball milling, when entering magnetic separator, ore deposit pulp density is 30%.Ferronickel powder after magnetic separation is delivered in concentrate pond, and refuse ore reclaiming machine delivered to by other mineral aggregates, reclaims ferronickel powder further, is sent in tailings pond by isolated slag more afterwards.
Utilize the present invention 4 cover system, wherein rotary kiln specification is
, adopt the method for this embodiment to process 1400t every day, daily output ferronickel powder 280t, former red soil nickel ore consume fuel coal 35kg per ton, reductive agent and limestone powder consume 140kg altogether.Within every 4 hours, detect the ferronickel powder sample obtained, continue 1 year, nickel grade is all more than 11%, and nickel recovery is all more than 92%, and Iron grade is all more than 82%, and iron recovery is being all more than 85%.
In addition, when adopting this embodiment method to prepare ferronickel powder, in rotary kiln, the viscosity of liquid phase keeps good, and kiln wall is long thick ring formation not easily, and average one is only and need clears up 2 times, thus adds production efficiency.
Embodiment 2
This embodiment is except have adjusted except the consumption of limestone powder in mixing step, and other are all identical with embodiment 1, and the mass ratio of dry ore deposit in the present embodiment, reductive agent pulverized anthracite and limestone powder is 85:8:7.
Adopt the present embodiment method to glue kiln phenomenon relatively seriously, kiln wall is long thick ring formation easily, within average 1 year, need clear up 5-6 ring formation.
In the nickel fine powder that this embodiment method obtains, nickel grade is all more than 10%, and nickel recovery is all more than 90%, and Iron grade is all more than 81%, and iron recovery is being all more than 83%.
As known by the technical knowledge, the present invention can be realized by other the embodiment not departing from its spirit or essential feature.Therefore, above-mentioned disclosed embodiment, with regard to each side, all just illustrates, is not only.Within the scope of the present invention all or be all included in the invention being equal to the change in scope of the present invention.
Claims (10)
1. the method for a direct reduction of laterite nickel mine with rotary kiln production ferronickel powder, it is characterized in that, comprise primary crushing, oven dry, second time fragmentation, mixing, pressure ball, rotary kiln baking reduction, third time fragmentation, ball milling and first time magnetic separation step, finally obtain ferronickel powder, wherein:
In described primary crushing step, it is below 80mm that raw material red soil nickel ore is crushed to raw meal particle size;
In described baking step, dried by the red soil nickel ore after primary crushing, described bake out temperature is 750 DEG C ~ 850 DEG C, and drying time is 15-25min;
In described second time destruction step, by red soil nickel ore secondary breaking to the raw meal particle size after drying be below 3mm account for more than 80%, thus obtain the suitable dry ore deposit of granularity;
In described mixing step, described dry ore deposit is mixed with reductive agent carbon, limestone powder, add water simultaneously, thus formation mixture, wherein, described dry ore deposit accounts for the 85-92wt% of described dry ore deposit, reductive agent carbon and limestone powder gross weight, and described reductive agent carbon accounts for the 5-12wt% of described dry ore deposit, reductive agent carbon and limestone powder gross weight, described limestone powder accounts for the 1-3wt% of described dry ore deposit, reductive agent carbon and limestone powder gross weight, and the water content of described mixture is 14-16wt%;
In described pressure ball step, described mixture is pressed into pelletizing;
In described rotary kiln baking reduction step, described pelletizing is sent in rotary kiln from rotary kiln feed-pipe, after super-dry, preheating, reducing roasting three phases, falls into dragveyer from kiln hood exit carry out Water Quenching, thus obtain agglomerate; Wherein, the temperature of described dryer section controls at 200 ~ 350 DEG C; The temperature of described preheating section controls at 350 ~ 600 DEG C; The temperature of described reducing roasting section controls at 600 ~ 1350 DEG C, and the total time that described pelletizing stops in whole rotary kiln is 4-6h.
2. method according to claim 1, is characterized in that, in described baking step, the partial heat described in drying plant is from the waste heat at described rotary kiln mouth place.
3. method according to claim 1, is characterized in that, in described pressure ball step, described pelletizing is of a size of 43 × 42 × 25mm.
4. method according to claim 1, is characterized in that, in described rotary kiln baking reduction step, described pelletizing is 2.5-3h in the time that described reducing roasting section stops.
5. method according to claim 1, is characterized in that, the specification of described rotary kiln is the inclined type rotary rotary kiln of Ф 3.6 × 72m, and the gradient of rotary kiln is 2.5%, and kiln body rotating speed is 0.2-1.8r/min.
6. method according to claim 1, is characterized in that, in described rotary kiln baking reduction step, the heat of described rotary kiln comes from the heat of injection from kiln head bunker coal burning generation.
7. method according to claim 1, is characterized in that, in described third time destruction step, described agglomerate is carried out be crushed to raw meal particle size be below 3mm account for more than 90%.
8. method according to claim 1, is characterized in that, in described ball milling step, the agglomerate after third time fragmentation carries out wet ball grinding, after ball milling the granularity of agglomerate be below 120 orders account for more than 80%.
9. method according to claim 1, is characterized in that, in described first time magnetic separation step, the ore deposit pulp density entering magnetic separator is 25-30%, after described first time magnetic separation, obtain high-grade ferronickel powder.
10. method according to claim 1, it is characterized in that, tramp iron separator magnetic separation step is set between described third time fragmentation and described ball milling, adopts tramp iron separator to carry out magnetic separation to the agglomerate after described third time fragmentation, to select part of nickel iron powder from the broken last agglomerate after third time fragmentation.
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| CN106702163A (en) * | 2016-12-23 | 2017-05-24 | 宝钢德盛不锈钢有限公司 | Method for recovering harmless ferronickel alloys from stainless steel sludge |
| CN106755963A (en) * | 2016-12-23 | 2017-05-31 | 宝钢德盛不锈钢有限公司 | A kind of method of dilval in high efficiente callback stainless steel sludge |
| CN108034811A (en) * | 2017-12-26 | 2018-05-15 | 江苏省冶金设计院有限公司 | A kind of method for producing metallic nickel iron powder and diopside matter ground-slag |
| CN110144470A (en) * | 2019-06-06 | 2019-08-20 | 李朝侠 | Lateritic nickel ore rotary kiln restores-blows smelting flow process |
| CN111850218A (en) * | 2020-06-23 | 2020-10-30 | 北京科技大学 | Method for smelting laterite-nickel ore by using HIsmelt smelting reduction process |
| CN112961954A (en) * | 2021-01-28 | 2021-06-15 | 江苏鹏飞集团股份有限公司 | Rotary kiln for producing ferronickel by directly reducing laterite-nickel ore and production method |
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| CN106636670A (en) * | 2016-12-12 | 2017-05-10 | 山西环能工程项目管理有限公司 | System and method for preparing ferronickel from laterite-nickel ore |
| CN106702163A (en) * | 2016-12-23 | 2017-05-24 | 宝钢德盛不锈钢有限公司 | Method for recovering harmless ferronickel alloys from stainless steel sludge |
| CN106755963A (en) * | 2016-12-23 | 2017-05-31 | 宝钢德盛不锈钢有限公司 | A kind of method of dilval in high efficiente callback stainless steel sludge |
| CN106755963B (en) * | 2016-12-23 | 2019-09-17 | 宝钢德盛不锈钢有限公司 | A kind of method of dilval in high efficiente callback stainless steel sludge |
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| CN108034811A (en) * | 2017-12-26 | 2018-05-15 | 江苏省冶金设计院有限公司 | A kind of method for producing metallic nickel iron powder and diopside matter ground-slag |
| CN110144470A (en) * | 2019-06-06 | 2019-08-20 | 李朝侠 | Lateritic nickel ore rotary kiln restores-blows smelting flow process |
| CN111850218A (en) * | 2020-06-23 | 2020-10-30 | 北京科技大学 | Method for smelting laterite-nickel ore by using HIsmelt smelting reduction process |
| CN112961954A (en) * | 2021-01-28 | 2021-06-15 | 江苏鹏飞集团股份有限公司 | Rotary kiln for producing ferronickel by directly reducing laterite-nickel ore and production method |
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